US3379624A - Process and equipment for the manufacture of pure polyalcohols - Google Patents

Process and equipment for the manufacture of pure polyalcohols Download PDF

Info

Publication number
US3379624A
US3379624A US381817A US38181764A US3379624A US 3379624 A US3379624 A US 3379624A US 381817 A US381817 A US 381817A US 38181764 A US38181764 A US 38181764A US 3379624 A US3379624 A US 3379624A
Authority
US
United States
Prior art keywords
evaporator
tmp
polyalcohol
polyalcohols
distillation
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US381817A
Other languages
English (en)
Inventor
Lindkvist Eirik
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Perstorp AB
Original Assignee
Perstorp AB
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Perstorp AB filed Critical Perstorp AB
Application granted granted Critical
Publication of US3379624A publication Critical patent/US3379624A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C31/00—Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
    • C07C31/18—Polyhydroxylic acyclic alcohols
    • C07C31/20—Dihydroxylic alcohols
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
    • C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
    • C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C35/00—Compounds having at least one hydroxy or O-metal group bound to a carbon atom of a ring other than a six-membered aromatic ring
    • C07C35/02—Compounds having at least one hydroxy or O-metal group bound to a carbon atom of a ring other than a six-membered aromatic ring monocyclic
    • C07C35/08—Compounds having at least one hydroxy or O-metal group bound to a carbon atom of a ring other than a six-membered aromatic ring monocyclic containing a six-membered rings
    • C07C35/14—Compounds having at least one hydroxy or O-metal group bound to a carbon atom of a ring other than a six-membered aromatic ring monocyclic containing a six-membered rings with more than one hydroxy group bound to the ring
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2601/00—Systems containing only non-condensed rings
    • C07C2601/12—Systems containing only non-condensed rings with a six-membered ring
    • C07C2601/14—The ring being saturated

Definitions

  • the polyalcohols employed in this invention are primarily trimethylolpropane (TMP), trimethylolethane (TME), tetramethylolcyclo'hexanol (TMC) and anhydroenueaheptitol (AEI-l).
  • the purifying of the polyalcohol obtained on vacuum evaporation of the synthesized product has up to now been carried out mainly by crystallization or distillation.
  • the extraction is usually performed by mean-s of alcohols, ketones or esters as solvents. This solvent must be volatilized afterwards, which means an economical burden.
  • the evaporated polyialcohol is centrifuged at sufficiently high temperature, eg. 70- 100'C., to separate the polyalcohol as a low viscosity liquid.
  • the alcohol is then ⁇ diluted'with water and is passed through an ion exchanger for further purifying. This process is described in detail in the Swedish Patent No. 181,290.
  • Still another process for purifying polyalcohols relates to a process in which the alcohol, which has been purified by centrifuging and ion exchanging, is submitted to fractional distillation to obtain highly pure alcohol in a good yield. Since these processes are all continuous, the poly'alcohol must stay for a very long time at 'high temperature, e.g. 12 hours at 180 C. during the fractional distillation. This very long hold-up causes many practical disadvantage-s and additionally gives -rise to thermal decomposition (cracking), discoloration of the product etc., which leads to a product of bad quality.
  • the purification of the described polyalcohols obtained by the described synthesis is accomplished by a process which comprise-s continuously evaporating the r-aw polyaloohol in a rapid evaporator and thereafter fractionally -distilling the vaporized product to remove a lower and a higher boiling fraction and to recover a polyalcohol of greatly improved purity.
  • the raw polyalcohol can be preliminarily purified by evapora-tion tand centrifugation.
  • the polyalcohol is sepa-ra-ted from remaining sodium or calcium formate together with other possible impurities, eg.
  • the polyalcohol in a rapid evaporator .such as .a thin layerevaporator an-d the polyalcohol is thereafter purified by fractional distillation.
  • the raw polyalcohol contains even after the centrifuging a substantial amount of ⁇ sodium or cialcium formate, which in prior art methods was separated by extraction or by ion exchanging.
  • this sodium or calcium formate is separated from the alcohol in a rapid evaporator of special 3,379,624 Patented Apr. 23, 1968 lCe construction, so that the ion exchangers and the extraction apparatus can be discarded.
  • the rapid evaporator according to the invention is preferably a so-ca'lled thin layer or film evaporator.
  • Such evaporators are constructed for separating liquids from each other. lt has therefore been necessary to change the construction of the thin layer evaporator so that it can separate solids from liquids :as required in the purification of the present invention.
  • the raw polyalcoh-ol such as TMP manufactured by condensation of butyraldehyde and formaldehyde in alkaline conditi-ons, is neutralized ybefore evaporating :and centrifuging and is thus also neutral at the input into the rapid evaporator.
  • the pH of the solution after neutralizing is regulated to approximately 4-8, preferably 5-6. Any fur-ther preliminary treatment of the raw neutral TMP to make this suitable for treatment in the thin layer evaporator is not required.
  • FIG. 1 is a flow diagram of apparatus for manufacturing TMP
  • FIG. 2 is a horizontal, sectional view of a thin layer evaporator according to the invention
  • FIG. 3 illustrates a feeding out device from the thin layer evaporator.
  • the raw polyalcohol, in this case TMP is contained in the intermediate container 1, which is held warm, e.g. C. by means of heating coils (not shown) to keep the TMP in the liquid state.
  • the intermediate container 1 the raw TMP is sucked via conduit 2 into the thin film evaporator 3, in which sodium or calcium formate and possibly other heavy constituents such as dimers of TMP are separated and fed out through the feeding out device 4.
  • the evaporator 3 a clear vapour of TMP is fed out through conduit 5.
  • the temperature in the evaporator is conveniently maintained within the range of l60-l80 C. and the pressure is maintained within the range of 2-5 mm. Hg.
  • the thin layer evaporator is heated in a common way for example by circulating a heat transferring liquid, eg. Dowtherm, in the surrounding jacket of the evaporator.
  • the amount of sodium or calcium formate, which is 4fed out of the bottom part of the evaporator, amounts upto approximately 4%, calculated on the TMP. This amount, however, may be considerably changed depending on whether the raw polyalcohol has been centrifuged in advance or not. It may in unfavourable cases amount up to 50%.
  • the sodium or calcium formate may
  • the hold-up time for the TMP in the thin layer evaporator is calculated to be about 10-60 seconds.
  • the lighter fractions are separated from the TMP and are conducted via the pipe 7 to the condenser 8, from which one part is returned via the conduit 9 to the column 6, and another part is conducted via the conduit 10 to the receiver 11.
  • the light fraction, which is gathered in the receiver 11, amounts to about 2-6% by weight calculated on the raw polyalcohol.
  • the column is heated in any common way for example by circulating a part of the liquid at the bottom through a heat exchanger.
  • the pressure in the distillation column is maintained within a range of 2-10 mm.
  • Hg and the temperature in the bottom part of the column is maintained at approximately C.
  • the Water temperature in the condenser is conveniently about 70 C.
  • the TMP which has been ifreed from the light constituents, is gathered in the bottom part 12 of the column and is fed via the conduit 13 to another column 14, in which the TMP is separated from the heavier constituents, which are gathered in the bottom part 15 and are pumped continuously via the pipe 16 to the receiver 17. This afterfraction amounts to approximately 610% by weight calculated on the raw polyalcohol. Also this column is filled with filler bodies, and the pressure is maintained within approximately 2-10 mm. Hg and the temperature is about 180 C.
  • the Vaporized TMP is fed out via the conduit 18 and is condensed in the condenser 19, from which one :part of the TMP is returned to the upper part of the column via the conduit 2t), while another part is conducted via the conduit 21 to an intermediate container or the like. Finally the TMP is optionally flaked in a conventional apparatus.
  • the pre-fraction and the afterfraction, which are stored in the receivers 11 and 17, respectively, may afterwards, if desired, be further purified separately to collect the amount of TMP contained in these fractions.
  • the TMP manufactured by this process is of a Very high quality. lt has a colour number, which may be as low as 0 APHA. As a comparison it may lbe mentioned that usual, commercially available TMP, has a colour number of -100 APHA.
  • the phthalic acid melt is also unusually light having a value of 1-3, measured in the colour scale ISK 1510 (Japanese colour scale).
  • the yield orf pure TMP obtained by the process according to the present invention is higher than the one obtained by prior art methods and comprises up to approximately 85-90% calculated on the basis of the starting materials formaldehyde and butyraldehyde.
  • the distance between the rotor and the inner wall is indicated by the letter a.
  • the rotor blades 52 are pivotally suspended in a ring 53. By the action of the centrifugal force they will scrape against the wall.
  • the rotor is normally rotated at 700-800 r.p.m. Since the evaporation in the thin layer evaporator is taking place under a very high vacuum, the sodium or calcium formate together with other solid substances therefore has to be sluiced out from the bottom of the thin layer evaporator. Suitable device for this purpose is Shown in FIG. 3. The solids fall via a pocket down into a space 71. The exit from this space is maintained closed by means of a vacuum tight closure 72.
  • the closure 73 is closed when the closure 72 must be opened for the removal of solids in order to maintain the vacuum in pocket 70. Additional solids are thus allowed to be gathered in the pocket 70 during the removal of solids from space 71.
  • the closure 73 is inclined in its closed position, while the closure 72 is arranged vertically.
  • the opening of the closures 72 and 73 is carried out by means of a programmed device 74.
  • a water jet 75 is arranged for facilitating the emptying of the space 71 by rinsing out the solids.
  • the advantages, which are obtained by the present invention, in addition to the ones mentioned above, are the 'very substantial economic advantages gained by avoiding the need for ion exchangers, the necessity to dilute the solution, the necessity to extract the product and similar preliminary purificatons.
  • the invention has been CII 4 described above in connection with a conventional process for manufacturing polyalcohols by which the water and the major part of the solids have been removed in advance.
  • the invention can be adapted also for purifying polyalcohols manufactured in other ways.
  • a pure polyalcohol selected from the group consisting of trimethylolpropane, trimethylolethane, tetramethylolcyclohexanol, and anhydroenneaheptitol, by reaction in alkaline media using formaldehyde, the steps which comprise continuously separating the raw polyalcohol from solid impurities in a thin film evaporator maintained at a pressure of about 2 to 5 mm.
  • Hg and a temperature of about 160 to 180 C. removing and condensing the crude polyalcohol overhead, continuously distilling the condensed product from the evaporator to remove a lower boiling by-product fraction, continuously re-distilling the bottoms product of said distillation, and recovering a distillate of pure polyalcohol and a higher boiling by-product fraction, said distilling and redistilling being conducted at a pressure of about 2 to 10 mm. Hg and a temperature of about 180 C.
  • the means for removing said solid by-product comprises a sealed chamber, a sleeve connecting said chamber with the thin layer evaporator, means for sealing said chamber from said sleeve, means for opening and sealing an outlet from said chamber, means operatively connecting said sealing means to control the simultaneous opening of one and closing of the other, and a jet for rinsing out solids in said chamber.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US381817A 1964-05-14 1964-07-10 Process and equipment for the manufacture of pure polyalcohols Expired - Lifetime US3379624A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
SE5885/64A SE322204B (de) 1964-05-14 1964-05-14

Publications (1)

Publication Number Publication Date
US3379624A true US3379624A (en) 1968-04-23

Family

ID=20267446

Family Applications (1)

Application Number Title Priority Date Filing Date
US381817A Expired - Lifetime US3379624A (en) 1964-05-14 1964-07-10 Process and equipment for the manufacture of pure polyalcohols

Country Status (4)

Country Link
US (1) US3379624A (de)
DE (1) DE1493048A1 (de)
GB (1) GB1085874A (de)
SE (1) SE322204B (de)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3878055A (en) * 1970-06-04 1975-04-15 Ppg Industries Inc Reclamation of spent glycol by distillation in the presence of a catalytic amount of alkali metal hydroxide
US4233267A (en) * 1977-01-18 1980-11-11 Fiberglas Canada Limited Combined batch reactor system and continuous distillation apparatus
US4935555A (en) * 1988-11-25 1990-06-19 Elias Carole L Purification of neopentyl glycol
US4999090A (en) * 1988-04-10 1991-03-12 Towa Chemical Industry Co., Ltd. Process for preparing trans-1,4-cyclohexanedimethanol and powder of the same
WO1992007815A1 (en) * 1990-10-29 1992-05-14 Eastman Kodak Company Process for the purification of hydroxypivalyl hydroxypivalate
US8686197B2 (en) 2009-08-07 2014-04-01 Lanxess Deutschland Gmbh Method for improving the color number of trimethylolpropane
EP4467530A4 (de) * 2022-01-20 2025-05-07 Mitsubishi Chemical Corporation Herstellungsverfahren für polyalkohol

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2837468A (en) * 1955-12-23 1958-06-03 Trojan Powder Co Purification of polyhydric alcohols
US2930818A (en) * 1960-03-29 Process for the purification of i
US3183274A (en) * 1956-10-09 1965-05-11 Celanese Corp Trimethylolpropane
US3259662A (en) * 1962-04-02 1966-07-05 Exxon Research Engineering Co Purification of trimethylolpropane

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2930818A (en) * 1960-03-29 Process for the purification of i
US2837468A (en) * 1955-12-23 1958-06-03 Trojan Powder Co Purification of polyhydric alcohols
US3183274A (en) * 1956-10-09 1965-05-11 Celanese Corp Trimethylolpropane
US3259662A (en) * 1962-04-02 1966-07-05 Exxon Research Engineering Co Purification of trimethylolpropane

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3878055A (en) * 1970-06-04 1975-04-15 Ppg Industries Inc Reclamation of spent glycol by distillation in the presence of a catalytic amount of alkali metal hydroxide
US4233267A (en) * 1977-01-18 1980-11-11 Fiberglas Canada Limited Combined batch reactor system and continuous distillation apparatus
US4390398A (en) * 1977-01-18 1983-06-28 Fiberglas Canada Limited Modified process for resin manufacturing using a continuous separate distillation column
US4999090A (en) * 1988-04-10 1991-03-12 Towa Chemical Industry Co., Ltd. Process for preparing trans-1,4-cyclohexanedimethanol and powder of the same
US4935555A (en) * 1988-11-25 1990-06-19 Elias Carole L Purification of neopentyl glycol
WO1992007815A1 (en) * 1990-10-29 1992-05-14 Eastman Kodak Company Process for the purification of hydroxypivalyl hydroxypivalate
US5209827A (en) * 1990-10-29 1993-05-11 Eastman Kodak Company Process for the purification of hydroxypivalyl hydroxypivalate
US8686197B2 (en) 2009-08-07 2014-04-01 Lanxess Deutschland Gmbh Method for improving the color number of trimethylolpropane
EP4467530A4 (de) * 2022-01-20 2025-05-07 Mitsubishi Chemical Corporation Herstellungsverfahren für polyalkohol

Also Published As

Publication number Publication date
SE322204B (de) 1970-04-06
GB1085874A (en) 1967-10-04
DE1493048A1 (de) 1969-02-13

Similar Documents

Publication Publication Date Title
US3644179A (en) Method and apparatus for continuous fractionation of tall oil and similar mixtures of organic substances with preliminary plural stage thin film evaporation
JP3934168B2 (ja) ビスフェノールａの精製法
US4167470A (en) Process and apparatus for solvent extraction of oil from oil-containing diatomite ore
US4209646A (en) Process for crystallizing an adduct of 2,2-di(4-hydroxyphenyl) propane and phenol
US3379624A (en) Process and equipment for the manufacture of pure polyalcohols
US2194851A (en) Dehydration of organic liquids by azeotropic distillation
US2866739A (en) Recovery of beta-sitosterol from tall oil pitch by steam distillation
US4239617A (en) Process and apparatus for solvent extraction of oil from oil-containing diatomite ore
NO329476B1 (no) Fremgangsmate og anlegg for separasjon og rensing av en ra blanding omfattende hydrokinon og resorcinol
US4154866A (en) Method of producing from wood tar a liquid smoke product for use in food processing, and product of said method
US4263102A (en) Process for the continuous recovery of thermally unstable solvent mixtures
CN108383702A (zh) 一种从山苍子头油中提取香茅醛的方法
US275128A (en) Impure anthraceinone and alizarine
US2431554A (en) Purification of vinyl acetate by distillation and scrubbing of the distillate
US3147199A (en) Steam
US3493469A (en) Distillation and decanting system for separating components
US2148579A (en) Recovery of fermentation products and the like
JP3917201B2 (ja) ビスフェノールａの製造方法
US1921157A (en) Purifying ethylene dibromide
US1826302A (en) Method for the dehydration of formic acid
US3519645A (en) Process for the preparation of propane-sultone
EP0153292B1 (de) Reinigung von roher Sorbinsäure
US2953504A (en) Method of separating acenaphthene, diphenylene oxide and fluorene from aromatic oils
US2806892A (en) Recovering trimethylolethane by ethyl acetate extraction
US2764595A (en) Process for the preparation of technically pure anthracene and carbazole from crude anthracene